US5573658A - Low brightness functional pigment from process by-product - Google Patents
Low brightness functional pigment from process by-product Download PDFInfo
- Publication number
- US5573658A US5573658A US08/365,627 US36562794A US5573658A US 5573658 A US5573658 A US 5573658A US 36562794 A US36562794 A US 36562794A US 5573658 A US5573658 A US 5573658A
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- US
- United States
- Prior art keywords
- kaolin
- clay
- pigment
- suspension
- brightness
- Prior art date
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- Expired - Lifetime
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
- C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
- C09C1/40—Compounds of aluminium
- C09C1/42—Clays
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
- D21H19/00—Coated paper; Coating material
- D21H19/36—Coatings with pigments
- D21H19/38—Coatings with pigments characterised by the pigments
- D21H19/40—Coatings with pigments characterised by the pigments siliceous, e.g. clays
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/51—Particles with a specific particle size distribution
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/60—Particles characterised by their size
- C01P2004/61—Micrometer sized, i.e. from 1-100 micrometer
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/60—Particles characterised by their size
- C01P2004/62—Submicrometer sized, i.e. from 0.1-1 micrometer
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/60—Optical properties, e.g. expressed in CIELAB-values
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
- C01P2006/82—Compositional purity water content
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T428/00—Stock material or miscellaneous articles
- Y10T428/31504—Composite [nonstructural laminate]
- Y10T428/31971—Of carbohydrate
- Y10T428/31993—Of paper
Definitions
- the present invention relates to mineral pigments for use in the paper industry and more particularly relates to a method of producing low brightness pigments from beneficiation process by-products.
- Natural occurring clays vary considerably in their color properties, even when produced from mines in the same locality or even from different sites in the same mine. Natural occurring kaolin clay deposits contain discoloring contaminants, for example, iron and titanium minerals. Titanium minerals in kaolin usually occur as discolored particles and these, coupled with iron oxides and other ferriferous material, are largely responsible for the yellow-brown shade of many kaolins. Often a clay is rejected as being unsuitable for commercial use solely on the basis of brightness even though its other physical properties, such as the viscosity of clay-water slurries and particle size, are within desired limits.
- discoloring contaminants for example, iron and titanium minerals. Titanium minerals in kaolin usually occur as discolored particles and these, coupled with iron oxides and other ferriferous material, are largely responsible for the yellow-brown shade of many kaolins. Often a clay is rejected as being unsuitable for commercial use solely on the basis of brightness even though its other physical properties, such as the viscosity of clay-
- a third process exemplified by U.S. Pat. No. 4,424,124 to Iannicelli involves the removal of iron oxides and iron stained TiO 2 impurities by magnetic separation. All three processes, selective sedimentation, DFA, and magnetic separation produce a substantial amount of reject material which have heretofore been discarded.
- a fourth process, not yet widely used, is called froth flotation which utilizes frothing agents to remove TiO 2 impurities. These froths rise to the surface and are removed to leave an improved brightness product.
- the present invention is directed to a process for producing a usable pigment from the reject material from the above processes or a similar process which produces a low brightness, titanium dioxide-rich reject.
- a method for producing a low brightness, high yellow index clay pigment from a clay containing iron-stained titanium dioxide is described.
- the clay is dispersed in water to create a kaolin dispersion which is separated into an aqueous high brightness fraction and an aqueous lower brightness fraction.
- This lower brightness fraction contains substantially 4-12% by weight of dry clay TiO 2 and substantially between 0.5-2.5% by weight of dry clay Fe 2 O 3 .
- the lower brightness fraction is concentrated to form a kaolin suspension which contains kaolin particles and iron-stained TiO 2 particles.
- the kaolin suspension is washed to remove excess salts to form a kaolin pigment slurry.
- a low brightness clay pigment which comprises kaolin particles containing substantially between 5-12% by weight of dry clay TiO 2 , substantially between 0.5-0.25% by weight of dry clay Fe 2 O 3 .
- This pigment has a TAPPI brightness substantially between 60 and 80.
- the present invention there is provided a method for producing pigments from reject kaolin which has been separated from the high brightness product flow stream.
- the present invention also provides for a novel pigment produced from the rejects of mineral beneficiating processes.
- pigments which can be utilized in the production of a variety of paper and paper board products.
- useful pigments are produced from kaolin clay by first dispersing the clay in a convenient manner well known in the art and then separating the dispersion into a high brightness, low yellow index fraction and a low brightness high yellow index fraction. This separation may be done by the separation methods discussed earlier, such as selective sedimentation, selective flocculation (DFA), magnetic separation or froth flotation, either alone or in combination.
- DFA selective flocculation
- froth flotation either alone or in combination.
- DFA selective flocculation
- froth flotation magnetic separation
- the lower brightness fractions were either reprocessed for further extraction of high brightness material or, if no more high brightness material could be extracted, discarded. It is a discovery of the present invention that these "rejects" can be made into a useful pigment.
- the clay particles and iron-stained TiO 2 in the low brightness fraction are concentrated to produce a mineral suspension. This concentration step permits the efficient handling and further processing of the pigment.
- Concentration may be achieved by filtration, frothing or sedimentation, but flocculation followed by hydro-separation with filtration is presently preferred. This produces a flocculent typically having a solids content of about 65 percent. If the DFA process is employed, it may be seen that separation of fractions and concentration of pigment is achieved simultaneously. If separation is achieved by magnetic separation, the "rejects" are already dispersed at low solids (1-3%) in the magnet flush water. If concentration is achieved by filtration, later dispersion may not be necessary. However, it is presently believed that flocculation of the pigment from the flush water would still be preferred. If separation is by selective sedimentation, the reject slurry may already be in a dispersed state at high enough solids for further processing. If not, it too may be flocculated or filtered. If the separation is achieved by froth flotation, the froth is substantially concentrated also, although further concentration may be desired.
- the pigment is thoroughly washed to remove excess salts accumulated in earlier processing. This washing may be achieved by elutriation of the flocculent at low solids and then filtered, centrifuged or by other means known to the art, but it is most preferred to disperse the concentrate (if a polymer floccule), dilute the slurry, screen, re-flocculate and filter as more fully described later.
- the pigment can be further washed on the filters by using sprays or multiple filtration. It should be noted that it is good practice during the process to periodically screen or "degrit" the concentrate slurry while it is in the dispersed, and often more dilute, state.
- the filter cake is dewatered. This may be achieved by redispersing the pigment, typically with an organic dispersant, and spray drying or drying the filter cake directly and milling. Alternatively, a portion of the dispersed pigment may be spray dried and blended back into the dispersion slurry to increase the solids content sufficiently for use as a slurried pigment.
- This more preferred embodiment for preparing useful low brightness, high yellow index pigments from kaolin involves dispersing a crude kaolin clay in water using excess dispersants and degritting as required. Following high shear mixing, additional salts, preferably sodium chloride, are added with dilution and the dispersion is aged. The dispersion is further diluted and flocculated with an anionic, high molecular weight polymer to separate the kaolin dispersion into a high brightness and low brightness fraction. The low brightness floccule, rich in iron-stained TiO 2 , is concentrated and removed by hydro-separation.
- DFA separation process see U.S. Pat. No. 3,857,781 to Maynard which is hereby incorporated by reference.
- the floccule so produced and heretofore termed "rejects", is redispersed at high shear agitation, adding a suitable dispersant, typically sodium hexametaphosphate.
- a suitable dispersant typically sodium hexametaphosphate.
- the solids Content during this agitation preferably should be adjusted to about 30-50 percent by weight, typically about 40%.
- the solids content thereof is adjusted as necessary in order that the dispersion may be degritted by passing it through a screening process. At this point the solids content should be adjusted to about 25 to 50 typically about 35%.
- the mineral slurry is reflocculated and filtered to remove excess salts. Reflocculation is achieved by adjusting the solids content between about 20 to about 30wt. % and adjusting the pH of the slurry to between about 3.0 and 5.5, with pH 4 being preferred. In a preferred embodiment the pH was initially adjusted to below about 5.5 by the addition of a strong acid, e.g. sulfuric acid. The final pH adjustment was achieved by the addition of alum. After filtering, the filter cake is then either redispersed and spray dried or acid dried and physically sized, e.g. by air classification, according to the desired final product characteristics. The resulting pigments contain 5-12% by weight TiO 2 and 0.5-2.5% Fe 2 O 3 . More typically, the pigment contains 7-10% TiO 2 and 1-2% Fe 2 O 3 . Throughout, all Ti and Fe compounds present are reported as if 100% in the form of its respective oxide.
- An alternative, through less preferred technique for removing excess salts from the TiO 2 rich floc involves elutriating or washing the flocs with water under low agitation conditions and then filtering and drying as described above.
- Many other techniques are well known in the industry to alternately disperse, flocculate and re-disperse to beneficiate kaolin slurries and these same techniques can be employed in practicing the present invention.
- the present process may be utilized to recover pigments from the rejects of a beneficiation process that utilizes polymers as flocculating agents.
- the initial starting material may be a mineral, such as a crude clay, which includes titanium and/or iron compound impurities.
- the titanium and/or iron compounds must first be concentrated.
- the clay In order to concentrate the iron-stained titanium impurities the clay must be subjected to a beneficiation process which causes the titanium impurities to be removed and concentrated.
- the preferred procedure for this concentration of titanium impurities follows the general procedure set forth in U.S. Pat. No. 3,857,781. That is, the mineral, e.g. clay, is dispersed, treated with a salt and aged. After aging with the salt, the dispersion is treated with a polymer which effects sedimentation of the titanium impurities by forming titanium polymer flocs which subsequently settle out.
- Preferred salts used for selective flocculation of the titanium impurities include sodium chloride, sodium sulfate, sodium carbonate, potassium chloride, sodium nitrate and ammonium chloride, with sodium chloride being more preferred.
- the amount of salt utilized to effectively treat clay mineral dispersions has been found to be between about 4-50 pounds per ton of dry clay, and more preferably about 12 pounds per ton of dry clay.
- the salt should be added to a 25-45 wt. % solids mineral dispersion, and more preferably to about a 40 wt. % solids mineral dispersion.
- the initial mineral dispersion may be produced by utilizing a suitable dispersion agent such as sodium hexametaphosphate and/or sodium metasilicate.
- the salt treated clay should be aged for a period of from 5 to 24 hours under static conditions. Otherwise the salt treated dispersion may be aged for 1 to 5 hours under mild agitation. The latter aging process is more suitable for commercial production.
- the dispersion should be adjusted to have a solids content between about 10 to 30 wt. %, and preferably 20 wt. %.
- the polymer flocculation agent is added at about 0.01 to 0.3 pounds per ton of dry clay to form iron-stained titanium-polymer flocs which settle out, thus forming the titania-rich clay concentrate utilized to produce the pigments according to the present invention.
- Preferred polymers utilized as flocculation agents include Nalco 635 and 675, a water soluble, strongly anionic, polyacrylamide polymer with a molecular weight in excess of one million, produced by Nalco Chemical Company, Chicago, Ill. and Betz 1200, 1210, 1220 and 1230, a water soluble, strongly anionic, organic copolymer of acrylamide having a molecular weight in excess of one million, available from Betz Laboratories, Inc., Trevose, Pa.
- Other suitable polymers employed comprise water soluble, strongly anionic products produced by the polymerization of acrylamides or copolymers of acrylamide and other monomers polymerizable therewith such as acrylic acid, methacrylic acid, etc.
- the present process is utilized to obtain a concentrate of titanium impurities for subsequent production of a pigment having a high concentration of titanium compounds.
- the properties of the "beneficiated" mineral or clay in the above process may be of little concern, since it may be subjected to other treatment processes. Accordingly, the process parameters may be selected to optimize or control the amount of titanium concentrated.
- a 55-gallon drum of polymer flocculated anatase reject material from a DFA hydroseparator underflow stream was used.
- the contents of the drum were agitated with a Lightnin-type mixer equipped with a marine-style impeller.
- the agitated contents were sampled and found to have 47.25 wt. % solids.
- the analytical technique utilized for determining the percent solids by specific gravity had to be modified to account for the density changes caused by flocculating the slurry with polymers. For this purpose, based on the previous processing of the clay, a correction factor of +0.3 g/100cc has used.
- the 653 pounds of slurry contained 308 pounds of bone dry, iron-stained TiO 2 rich clay.
- the slurry pH was measured at 10.4.
- the contents of the drum were transferred to a 30-inch diameter tank placed under a 25 H.P. Cowles dissolver installed with an 18-inch diameter dissolver blade.
- a 30-inch diameter tank placed under a 25 H.P. Cowles dissolver installed with an 18-inch diameter dissolver blade.
- one pound per ton B.D. clay lbs/TC
- sodium hexametaphosphate Calgon
- the Cowles dissolver was turning at 750 RPM, yielding a tip speed (on the 18-inch impeller blade) of 3534.3 feet per minute.
- the slurry was next transferred from the tank under the mixer through a screener and into a storage tank. In order to pass the slurry through the screener, it had to be diluted to about 40 wt. % solids.
- the necessary dilution was conducted by adding water to the slurry in the tank under the mixer.
- the slurry was pumped directly to a 48-inch diameter Midwestern vibrating screener, equipped with a 325 mesh screen.
- the material that passed through the screen was caught in a catch-bucket on the inlet to a centrifugal pump, which moved the material to a potbellied tank. A total of 77.7 gal. slurry was recovered. Analysis revealed a solids content of 36.27 wt.
- the purpose of the screening was to degrit the slurry. About one liter of grit was found to have remained on the screen at the end of the transfer.
- the exact solids content of the dispersed slurry was then used to dilute the slurry to a solids range of 22.5 to 23.5 wt. %. A solids content of 23.33 wt. % was actually achieved.
- This slurry was then flocculated by adding sulfuric acid (H 2 SO 4 ) until a pH of 5.03 was achieved, and then adding alum to a pH of 3.9. This resulted in the addition of 7.5 lbs acid/ton B.D. clay, and 6.0 lbs alum/ton clay (dry basis).
- the filter cake was placed in a small tank, under a small Cowles Dissolver and dispersed in two batches. To each batch was added 9.2 lbs./TC fresh as-received Colloid 211, and 4.1 lbs./TC soda ash to disperse the filtered cake.
- the slurry pH was 6.9 (target range was 6.8-7.2). In addition, sufficient water was added to reduce the solids content down to 52wt. %, to facilitate screening. Tip speed on the small Cowles dissolver was maintained at about 3500 RPM. The slurry was screened again, through 325 mesh screen, and then spray dried.
- Outlet temperature was held at 220° F. by varying the feed rate, and the inlet temperature was maintained at 1000° F. by varying the gas to the air heater.
- Product data is given in Table II below.
- the clay made by the above-described process may be utilized as a coating in applications wherein high brightness is not required.
- clay processed by the present invention is usable as a precoat for a paper or paperboard with low brightness base stock.
- the use of the low (60-80 TAPPI) brightness clay reduces the contrast between the coating and the base stock, thereby reducing the mottled appearance of the finished sheet.
- the iron-stained titanium dioxide present in the clay pigment due to the concentration effect of prior processing (5-12% by weight) gives hiding power superior to that attainable with clay alone.
- the brightness of the coating would increase and the mottling would be exaggerated due to the uneven coating distribution over the rough, unbleached fiber surface.
- a dye or colorant would have to be added to the coating. This procedure reduces the contrast between the coating and the base stock.
- the product of the present invention would be used without additional titanium dioxide and without dyes or colorants.
- the product of the present invention has also been discovered to be particularly useful in woodfree paper grades.
- the use of greater amounts of calcium carbonate in coatings today for woodfree premium paper grades may .result in the finished sheet exceeding the brightness limit for a specific grade.
- base sheet brightness cannot be varied in the pulp mill and be cost-effective.
- the coating formulation therefore, must be the agent of change. Dyes and colorants can control the brightness and shade but the pigment of the present invention will not only control shade and color, it will act as a kaolin clay pigment, providing improved coated sheet properties such as paper gloss, and improved print quality, as clay yields better printed gloss than calcium carbonate.
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- Chemical & Material Sciences (AREA)
- Dispersion Chemistry (AREA)
- Organic Chemistry (AREA)
- Paper (AREA)
- Pigments, Carbon Blacks, Or Wood Stains (AREA)
Abstract
Description
TABLE I ______________________________________ Filtration area 3.14 ft.sup.2 Drum speed 1.7 RPM Cloth, porosity 4-6 cfm Vacuum 22-24 in Hg Wet filter cake 96 lbs/m Cake solids 60.13% Dry clay 57.7 lbs/hr Filtration rate 18.4 lbs dry clay/hr/ft.sup.2 Filtrate solids 0.38% ______________________________________
TABLE II ______________________________________ Spray dried moisture 0.6% Brightness (TAPPI T-534) 71.6 Whiteness 32.8 Yellowness 15.2 +325 mest grit 0.002% Chemical Analysis TiO.sub.2 8.1% Fe.sub.2 O.sub.3 1.5% Al.sub.2 O.sub.3 36.5% SiO.sub.2 43.7% Particle Size (Sedigraph) +10μ 4.5% +5μ 16.0% -2μ 64.5% -1μ 55.0% -0.5μ 46.0% -0.2μ 25.5% ______________________________________
Claims (8)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US08/365,627 US5573658A (en) | 1991-01-18 | 1994-12-28 | Low brightness functional pigment from process by-product |
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US07/643,885 US5154767A (en) | 1991-01-18 | 1991-01-18 | Low brightness functional pigment from process by-product |
US07/875,792 US5385239A (en) | 1991-01-18 | 1992-04-27 | Low brightness functional pigment from process by-product |
US08/365,627 US5573658A (en) | 1991-01-18 | 1994-12-28 | Low brightness functional pigment from process by-product |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US07/875,792 Continuation US5385239A (en) | 1991-01-18 | 1992-04-27 | Low brightness functional pigment from process by-product |
Publications (1)
Publication Number | Publication Date |
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US5573658A true US5573658A (en) | 1996-11-12 |
Family
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Family Applications (4)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US07/643,885 Expired - Lifetime US5154767A (en) | 1991-01-18 | 1991-01-18 | Low brightness functional pigment from process by-product |
US07/875,894 Expired - Lifetime US5190615A (en) | 1991-01-18 | 1992-04-27 | Low brightness functional pigment from process by-product |
US07/875,792 Expired - Lifetime US5385239A (en) | 1991-01-18 | 1992-04-27 | Low brightness functional pigment from process by-product |
US08/365,627 Expired - Lifetime US5573658A (en) | 1991-01-18 | 1994-12-28 | Low brightness functional pigment from process by-product |
Family Applications Before (3)
Application Number | Title | Priority Date | Filing Date |
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US07/643,885 Expired - Lifetime US5154767A (en) | 1991-01-18 | 1991-01-18 | Low brightness functional pigment from process by-product |
US07/875,894 Expired - Lifetime US5190615A (en) | 1991-01-18 | 1992-04-27 | Low brightness functional pigment from process by-product |
US07/875,792 Expired - Lifetime US5385239A (en) | 1991-01-18 | 1992-04-27 | Low brightness functional pigment from process by-product |
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US (4) | US5154767A (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6068693A (en) * | 1997-06-16 | 2000-05-30 | Ecc International Inc. | Method for separating mixture of finely divided minerals and product thereof |
US6615987B1 (en) | 1999-05-07 | 2003-09-09 | Imerys Pigments, Inc. | Method of treating an aqueous suspension of kaolin |
US20040149407A1 (en) * | 2001-06-25 | 2004-08-05 | Chen Gordon Cheng | Manufacture of paper and paper board |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5154767A (en) * | 1991-01-18 | 1992-10-13 | J. M. Huber Corporation | Low brightness functional pigment from process by-product |
GB9405275D0 (en) * | 1994-03-17 | 1994-04-27 | Ecc Int Ltd | Aqueous suspensions of inorganic materials |
US5713998A (en) * | 1995-02-14 | 1998-02-03 | Ecc International Inc. | Method for producing high opacifying kaolin pigment |
US5584394A (en) * | 1995-03-15 | 1996-12-17 | Engelhard Corporation | Colored titaniferous coating pigment obtained as a flocculated by-product in a kaolin purification process |
US5891236A (en) * | 1997-04-23 | 1999-04-06 | Thiele Kaolin Company | Process for improving the color and brightness of discolored goethite-containing materials |
US5810998A (en) * | 1997-06-05 | 1998-09-22 | Thiele Kaolin Company | Process for improving the brightness of fine-grained kaolin clays |
US6186335B1 (en) * | 1998-03-20 | 2001-02-13 | Thiele Kaolin Company | Process for beneficiating kaolin clays |
US6713038B2 (en) | 2000-04-18 | 2004-03-30 | Millenium Inorganic Chemicals, Inc. | TiO2 compounds obtained from a high silica content ore |
GB0622106D0 (en) | 2006-11-06 | 2006-12-20 | Imerys Minerals Ltd | Grinding and beneficiation of brucite |
US8967383B1 (en) | 2012-10-19 | 2015-03-03 | KaMin, LLC | Processes for producing high-brightness kaolin in high yields, and kaolin materials produced therefrom |
Citations (23)
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US3171718A (en) * | 1962-02-16 | 1965-03-02 | Freeport Sulphur Co | Delaminated domestic sedimentary clay products and method of preparation thereof |
US3343973A (en) * | 1966-06-30 | 1967-09-26 | Thiele Kaolin Co | Fractured clay |
US3371988A (en) * | 1967-08-25 | 1968-03-05 | Huber Corp J M | Method of beneficiating clay by removal of titanium impurities |
US3446348A (en) * | 1965-10-15 | 1969-05-27 | Freeport Sulphur Co | Process for treating clay |
US3528769A (en) * | 1966-11-15 | 1970-09-15 | Georgia Kaolin Co | Method of treating secondary kaolin |
US3536264A (en) * | 1968-06-11 | 1970-10-27 | Thiele Kaolin Co | Removal of titanium impurities from clay |
US3615806A (en) * | 1968-12-10 | 1971-10-26 | Georgia Kaolin Co | Kaolin pigments and methods of producing the same |
US3635662A (en) * | 1969-12-05 | 1972-01-18 | Georgia Kaolin Co | Kaolin product and method of producing the same |
US3661515A (en) * | 1970-05-18 | 1972-05-09 | Huber Corp J M | Method of brightening kaolin clay by removing organic contaminants |
US3701417A (en) * | 1970-09-28 | 1972-10-31 | Engelhard Min & Chem | Purification of clay by selective flocculation |
US3736165A (en) * | 1971-07-21 | 1973-05-29 | Minerals & Chemicals Corp | Method for processing kaolin clay |
US3737333A (en) * | 1971-07-21 | 1973-06-05 | Engelhard Min & Chem | Method for processing kaolin clay |
US3857781A (en) * | 1972-06-08 | 1974-12-31 | Huber Corp J M | Method of rapid differential flocculation of tio{11 from kaolin slurries |
US3862027A (en) * | 1972-06-13 | 1975-01-21 | Engelhard Min & Chem | Purification of clay by selective flocculation |
US4014705A (en) * | 1971-11-03 | 1977-03-29 | Pilkington Brothers Limited | Glass compositions |
US4227920A (en) * | 1978-07-18 | 1980-10-14 | Yara Engineering Corporation | Methods of clay benefication |
US4309222A (en) * | 1980-10-09 | 1982-01-05 | Pfizer Inc. | Kaolin clay slurries of reduced viscosity |
US4424124A (en) * | 1970-03-13 | 1984-01-03 | J. M. Huber Corporation | Method and magnetic separator for removing weakly magnetic particles from slurries of minute mineral particles |
US4812299A (en) * | 1986-06-17 | 1989-03-14 | J. M. Huber Corporation | Synthetic alkali metal alumino-silicates, methods and uses, compositions and their methods of preparation |
US4971629A (en) * | 1989-10-04 | 1990-11-20 | Ecc America Inc. | Method of preparing aggregated pigments from clays |
US5047375A (en) * | 1988-12-22 | 1991-09-10 | Ecc America Inc. | Method for producing high opacifying kaolin pigment |
US5154767A (en) * | 1991-01-18 | 1992-10-13 | J. M. Huber Corporation | Low brightness functional pigment from process by-product |
US5393340A (en) * | 1992-08-26 | 1995-02-28 | Engelhard Corporation | Metakaolin pigment with high brightness and low abrasion and manufacture thereof from soft kaolin clays |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2059811B (en) * | 1979-10-15 | 1983-01-06 | English Olays Lovering Pochin | Beneficiation of minerals |
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1991
- 1991-01-18 US US07/643,885 patent/US5154767A/en not_active Expired - Lifetime
-
1992
- 1992-04-27 US US07/875,894 patent/US5190615A/en not_active Expired - Lifetime
- 1992-04-27 US US07/875,792 patent/US5385239A/en not_active Expired - Lifetime
-
1994
- 1994-12-28 US US08/365,627 patent/US5573658A/en not_active Expired - Lifetime
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Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6068693A (en) * | 1997-06-16 | 2000-05-30 | Ecc International Inc. | Method for separating mixture of finely divided minerals and product thereof |
US6235107B1 (en) | 1997-06-16 | 2001-05-22 | Imerys Pigments, Inc. | Method for separating mixture of finely divided minerals and product thereof |
US6615987B1 (en) | 1999-05-07 | 2003-09-09 | Imerys Pigments, Inc. | Method of treating an aqueous suspension of kaolin |
US20040149407A1 (en) * | 2001-06-25 | 2004-08-05 | Chen Gordon Cheng | Manufacture of paper and paper board |
US7364641B2 (en) | 2001-06-25 | 2008-04-29 | Ciba Specialty Chemicals Water Treatments Ltd. | Manufacture of paper and paper board |
Also Published As
Publication number | Publication date |
---|---|
US5154767A (en) | 1992-10-13 |
US5385239A (en) | 1995-01-31 |
US5190615A (en) | 1993-03-02 |
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